EP1954660A2 - Isomerisation d'olefines - Google Patents

Isomerisation d'olefines

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Publication number
EP1954660A2
EP1954660A2 EP06826455A EP06826455A EP1954660A2 EP 1954660 A2 EP1954660 A2 EP 1954660A2 EP 06826455 A EP06826455 A EP 06826455A EP 06826455 A EP06826455 A EP 06826455A EP 1954660 A2 EP1954660 A2 EP 1954660A2
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Prior art keywords
group
chain
straight
branched
optionally substituted
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German (de)
English (en)
Inventor
Mark Andrew Harmer
Christopher P. Junk
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EIDP Inc
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EI Du Pont de Nemours and Co
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/23—Rearrangement of carbon-to-carbon unsaturated bonds
    • C07C5/25—Migration of carbon-to-carbon double bonds
    • C07C5/2506—Catalytic processes
    • C07C5/2525—Catalytic processes with inorganic acids; with salts or anhydrides of acids
    • C07C5/2531—Acids of sulfur; Salts thereof; Sulfur oxides
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/23—Rearrangement of carbon-to-carbon unsaturated bonds
    • C07C5/25—Migration of carbon-to-carbon double bonds
    • C07C5/2506—Catalytic processes
    • C07C5/2562—Catalytic processes with hydrides or organic compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • C07C2527/02—Sulfur, selenium or tellurium; Compounds thereof
    • C07C2527/053—Sulfates or other compounds comprising the anion (SnO3n+1)2-
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2531/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • C07C2531/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
    • C07C2531/025—Sulfonic acids

Definitions

  • This invention relates to a process for isomerizing olefins; the reaction is carried out in the presence of at least one ionic liquid.
  • BACKGROUND The isomerization of olefins to internal olefins is an important reaction in the refining industry.
  • Long chain olefins for example, can be isomerized to the internal olefins, which can be used as precursors to materials used in lubrication.
  • Ionic liquids are liquids composed of ions that are liquid around or below 100 0 C (Science (2003) 302:792-793).
  • Ionic liquids exhibit negligible vapor pressure, and with increasing regulatory pressure to limit the use of traditional industrial solvents due to environmental considerations such as volatile emissions and aquifer and drinking water contamination, much research has been devoted to designing ionic liquids that could function as replacements for conventional solvents.
  • the present invention provides a process for carrying out isomerization reactions using ionic liquids as solvent.
  • the use of at least one ionic liquid as the solvent for this reaction allows for ready separation of the product(s) from the catalyst.
  • the present invention relates to a process for making internal olefins comprising:
  • reaction mixture comprising (1) at least one ⁇ -olefin having from 4 to 25 carbons, (2) at least one acid catalyst selected from the group consisting of rare earth fluorinated alkyl sulfonates, organic sulfonic acids, fluoroalkyl sulfonic acids, metal sulfonates, metal trifluoroacetates, and combinations thereof, and (3) at least one ionic liquid having the Formula Z + A ' , wherein Z + and A " are defined in the Detailed Description; thereby forming an isomer phase comprising at least one internal olefin and an ionic liquid phase that comprises the at least one acid catalyst; and
  • Figure 1 shows the reaction mixture produced from contacting 1- dodecene with 1,1,2,2-tetrafluoroethanesulfonic acid in the presence of an ionic liquid.
  • Figure 2 shows the two-phase product obtained by contacting 1- dodecene with 1 ,1 ,2,2-tetrafluoroethanesulfonic acid.
  • Figure 3 is a GC tracing of the isomer phase obtained from the isomerization of 1-dodecene in the presence of the catalyst 1 ,1 ,2,2- tetrafluoroethanesulfonic acid and the ionic liquid 1-dodecyl-3- methylimidazolium 1 , 1 ,2,2-tetrafluoroethanesulfonate.
  • Figure 4 is a GC tracing of the reaction products obtained from the isomerization of 1-dodecene in the presence of the catalyst 1 ,1 ,2,2- tetrafluoroethanesulfonic acid (no ionic liquid present).
  • Figure 5 is a GC tracing of the isomer phase obtained from the isomerization of 1-dodecene in the presence of the catalyst 1 ,1 ,2,2- tetrafluoroethanesulfonic acid and the ionic liquid 1-octadecyl-3- methylimidazolium 1 ,1 ,2,2-tetrafluoroethanesulfonate.
  • the present invention relates to a process for isomerizing ⁇ -olefins in the presence of an ionic liquid solvent.
  • an ionic liquid as the solvent for the isomerization reaction is advantageous because the acid catalyst is recovered in an ionic liquid phase that is separate from the phase comprising the product isomer(s), thus the product isomer(s) are easily separated from the acid catalyst.
  • ionic liquid is meant an organic salt that is liquid around or below 100 0 C.
  • fluoroalkyl is meant an alkyl group wherein at least one member selected from the hydrogens has been replaced by fluorine.
  • perfluoroalkyl is meant an alkyl group wherein all of the hydrogens have been replaced by fluorines.
  • alkoxy is meant a straight-chain or branched alkyl group bound via an oxygen atom.
  • fluoroalkoxy is meant an alkoxy group wherein at least one member selected from the hydrogens has been replaced by fluorine.
  • perfluoroalkoxy is meant an alkoxy group wherein all of the hydrogens have been replaced by fluorines.
  • halogen is meant bromine, iodine, chlorine or fluorine.
  • heteroaryl is meant an aryl group having one or more heteroatoms.
  • catalyst is meant a substance that affects the rate of the reaction but not the reaction equilibrium, and emerges from the process chemically unchanged.
  • substituted C 2 H 5 may be, without limitations, CF 2 CF 3 , CH 2 CH 2 OH or CF 2 CF 2 I.
  • Ci to Cn straight-chain or branched where n is an integer defining the length of the carbon chain, is meant to indicate that Ci and C 2 are straight-chain, and C 3 to C n may be straight-chain or branched.
  • the invention provides a process for making internal olefins comprising:
  • reaction mixture comprising (1) at least one ⁇ - olefin having from 4 to 25 carbons, (2) at least one acid catalyst selected from the group consisting of rare earth fluorinated alkyl sulfonates, organic sulfonic acids, fluoroalkyl sulfonic acids, metal sulfonates, metal trifluoroacetates, and combinations thereof, and (3) at least one ionic liquid having the Formula Z + A " , wherein Z + is a cation selected from the group consisting of:
  • R 1 , R 2 , R 3 , R 4 , R 6 and R 6 are independently selected from the group consisting of:
  • R 7 , R 8 , R 9 , and R 10 are independently selected from the group consisting of:
  • substituted aryl or substituted heteroaryl has one to three substituents independently selected from the group consisting of
  • a " is R 11 -SO 3 - or (R 12 -SO 2 ) 2 N-; wherein R 11 and R 12 are independently selected from the group consisting of:
  • Z + is imidazolium or phosphonium.
  • a ' is selected from the group consisting of: [CH 3 OSO 3 ]-, [C 2 H 5 OSO 3 ]-, [CF 3 SO 3 ]-, [HCF 2 CF 2 SO 3 ]-, [CF 3 HFCCF 2 SO 3 ]-, [HCCIFCF 2 SO 3 ]-, [(CF 3 SO 2 J 2 N]-, [(CF 3 CF 2 SO 2 ) 2 N]-,
  • the ionic liquid Z + A " is selected from the group consisting of 1-butyl-2,3-dimethylimidazolium 1 , 1 ,2,2-tetrafluoroethanesulfonate, 1 -butyl-methylimidazolium 1 , 1 ,2,2- tetrafluoroethanesulfonate, 1-ethyl-3-methylimidazolium 1 ,1 ,2,2- tetrafluoroethanesulfonate, 1-ethyl-3-methylimidazolium 1 ,1 ,2,3,3,3- hexafluoropropanesulfonate, 1-hexyl-3-methylimidazolium 1 ,1 ,2,2- tetrafluoroethanesulfonate, 1 ⁇ dodecyl-3-methylimidazolium 1 ,1 ,2,2- tetrafluoroethanesulfonate, 1-he
  • the ⁇ -olefin starting material comprises from about four carbons to about twenty-five carbons.
  • the ⁇ -olefin starting material may comprise from about 12 carbons to about 18 carbons.
  • the starting material may comprise either linear or branched olefins, however preferably the starting material will comprise greater than 60 mol% linear ⁇ -olefin.
  • the starting material may also comprise from about 10 mol% to about 35 mol% branched ⁇ -olefin, from about 0 mol% to about 10 mol% linear internal olefin, and/or from about 0 mol% to about 10 mol% branched internal olefin.
  • the olefin starting material may also be admixed with one or more inert hydrocarbons, such as paraffins, cycloparaffins, or aromatics, however preferably, the olefin starting material comprises at least 90% by weight of olefins.
  • the at least one acid catalyst usable in the current process is selected from the group consisting of rare earth flubrinated alkyl sulfonates, organic sulfonic acids, fluoroalkyl sulfonic acids, metal sulfonates, metal trifluoroacetates, and combinations thereof.
  • the at least one acid catalyst is selected from the group consisting of:
  • R 13 is selected from the group consisting of:
  • Ci to C- I5 preferably C 3 to C 6 , straight-chain or branched fluoroalkyl, optionally substituted with at least one member selected from the group consisting of Cl, Br, I, OH, NH 2 and SH; (5) C 1 to C 15 , preferably C 3 to C 6 , straight-chain or branched fluoroalkoxy, optionally substituted with at least one member selected from the group consisting of Cl, Br, I, OH, NH 2 and SH;
  • R 14 is selected from the group consisting of:
  • Ci to Ci 5 preferably C 3 to C 6 , straight-chain or branched fluoroalkoxy, optionally substituted with at least one member selected from the group consisting of Cl, Br, I, OH, NH 2 and SH; and
  • Ci preferably C 3 to C 6 , straight-chain or branched perfluoroalkoxy
  • R 15 is selected from the group consisting of:
  • Ci to Ci 5 preferably C 3 to C 6 , straight-chain or branched fluoroalkyl, optionally substituted with at least one member selected from the group consisting of CI, Br 1 I, OH, NH 2 and SH;
  • Ci to Ci 5 preferably C 3 to C 6 , straight-chain or branched fluoroalkoxy, optionally substituted with at least one member selected from the group consisting of CI, Br, I, OH, NH 2 and SH; (6) Ci to C- I5 , preferably C 3 to C 6 , straight-chain or branched perfluoroalkyl; and (7) Ci to C-is, preferably C 3 to C 6 , straight-chain or branched perfluoroalkoxy.
  • the at least one acid catalyst is 1 , 1 ,2,2-tetrafluoroethanesulfonic acid, 1 ,1 , 2, 3,3,3- hexafluoropropanesulfonic acid, 2-chloro-1 ,1 ,2-trifluoroethanesulfonic acid, 1 ,1 ,2-trifluoro-2-(perfluoroethoxy)ethanesulfonic acid, 1 ,1 ,2-trifluoro- 2-(trifluoromethoxy)ethanesulfonic acid, or 1 ,1 ,2-trifluoro-2- (perfluoropropoxy)ethanesulfonic acid.
  • Most of the catalysts may be obtained commercially.
  • the at least one acid catalyst is used at a concentration of from about 0.1% to about 20% by weight of the total weight of the ⁇ -olefin(s) at the start of the reaction. In a more specific embodiment, the at least one acid catalyst is used at a concentration of from about 0.1% to about 10% by weight of the total weight of the ⁇ -olefin(s) at the start of the reaction. In an even more specific embodiment, the at least one acid catalyst is used at a concentration of from about 0.1 % to about 5% by weight of the total weight of the ⁇ -olefin(s) at the start of the reaction.
  • the reaction is preferably carried out at a temperature of from about 5O 0 C to about 175°C. In a more specific embodiment, the reaction is carried out at a temperature of from about 50°C to about 120 0 C.
  • the reaction is preferably carried out under an inert atmosphere, such as nitrogen, argon or helium.
  • the reaction may be performed at atmospheric pressure, or at pressures above atmospheric pressure.
  • the time for the reaction will depend on many factors, such as the reactants, reaction conditions and reactor. One skilled in the art will know to adjust the time for the reaction to achieve optimal isomerization of the ⁇ -olefins.
  • fluoroalkyl sulfonate anions may be synthesized from perfluorinated terminal olefins or perfluorinated vinyl ethers generally according to the method of Koshar, ef a/. (J. Am. Chem. Soc. (1953) 75:4595-4596); in one embodiment, sulfite and bisulfite are used as the buffer in place of bisulfite and borax, and in another embodiment, the reaction is carried in the absence of a radical initiator. 1 ,1 ,2,2-
  • Tetrafluoroethanesulfonate, 1 ,1 ,2,3,3,3-hexafluoropropanesulfonate, 1 ,1 ,2-trifluoro-2-(trifluoromethoxy)ethanesulfonate, and 1 , 1 ,2-trifluoro-2- (pentafluoroethoxy)ethanesulfonate may be synthesized according to Kosnar, et al. ⁇ supra), with modifications.
  • Preferred modifications include using a mixture of sulfite and bisulfite as the buffer, freeze drying or spray drying to isolate the crude 1 ,1 ,2,2-tetrafluoroethanesulfonate and 1 ,1 ,2,3,3,3-hexafluoropropanesulfonate products from the aqueous reaction mixture, using acetone to extract the crude 1 ,1 ,2,2- tetrafluoroethanesulfonate and 1 ,1 ,2,3,3,3-hexafluoropropanesulfonate salts, and crystallizing 1 ,1 ,2-trifluoro-2-(trifluoromethoxy)ethanesulfonate and 1 ,1 ,2-trifluoro-2-(pentafluoroethoxy)ethanesulfonate from the reaction mixture by cooling.
  • the at least one ionic liquid useful for the invention may be obtained commercially, or may be synthesized using the cations and an
  • Solution #1 is made by dissolving a known amount of the halide salt of the cation in deionized water. This may involve heating to ensure total dissolution.
  • Solution #2 is made by dissolving an approximately equimolar amount (relative to the cation) of the potassium or sodium salt of the anion in deionized water. This may also involve heating to ensure total dissolution. Although it is not necessary to use equimolar quantities of the cation and anion, a 1:1 equimolar ratio minimizes the impurities obtained by the reaction.
  • the two aqueous solutions (#1 and #2) are mixed and stirred at a temperature that optimizes the separation of the desired product phase as either an oil or a solid on the bottom of the flask.
  • the aqueous solutions are mixed and stirred at room temperature, however the optimal temperature may be higher or lower based on the conditions necessary to achieve optimal product separation.
  • the water layer is separated, and the product is washed several times with deionized water to remove chloride or bromide impurities. An additional base wash may help to remove acidic impurities.
  • the product is then diluted with an appropriate organic solvent (chloroform, methylene chloride, etc.) and dried over anhydrous magnesium sulfate or other preferred drying agent.
  • the appropriate organic solvent is one that is miscible with the ionic liquid and that can be dried.
  • the drying agent is removed by suction filtration and the organic solvent is removed in vacuo. High vacuum is applied for several hours or until residual water is removed.
  • the final product is usually in the form of a liquid, and in any case are liquid around or below 100 0 C.
  • Solution #1 is made by dissolving a known amount of the halide salt of the cation in an appropriate solvent. This may involve heating to ensure total dissolution.
  • the solvent is one in which the cation and anion are miscible, and in which the salts formed by the reaction are minimally miscible; in addition, the appropriate solvent is preferably one that has a relatively low boiling point such that the solvent can be easily removed after the reaction.
  • Appropriate solvents include, but are not limited to, high purity dry acetone, alcohols such as methanol and ethanol, and acetonitrile.
  • Solution #2 is made by dissolving an equimolar amount (relative to the cation) of the salt (generally potassium or sodium) of the anion in an appropriate solvent, typically the same as that used for the cation. This may also involve heating to ensure total dissolution.
  • the two solutions (#1 and #2) are mixed and stirred under conditions that result in approximately complete precipitation of the halide salt byproduct (generally potassium halide or sodium halide); in one embodiment of the invention, the solutions are mixed and stirred at approximately room temperature for about 4-12 hours.
  • the halide salt is removed by suction filtration through an acetone/celite pad, and color can be reduced through the use of decolorizing carbon as is known to those skilled in the art.
  • the solvent is removed in vacuo and then high vacuum is applied for several hours or until residual water is removed.
  • the final product is usually in the form of a liquid, and in any case are liquid around or below 100 0 C.
  • the physical and chemical properties of ionic liquids can be specifically selected by choice of the appropriate cation and anion. For example, increasing the chain length of one or more alkyl chains of the cation will affect properties such as the melting point, hydrophilicity/lipophilicity, density and solvation strength of the ionic liquid.
  • Choice of the anion can affect, for example, the melting point, the water solubility and the acidity and coordination properties of the composition.
  • ionic liquids Effects of cation and anion on the physical and chemical properties of ionic liquids are known to those skilled in the art and are reviewed in detail by Wasserscheid and Keim (Angew. Chem. Int. Ed. (2000) 39:3772-3789) and Sheldon (Chem. Commun. (2001) 2399-2407).
  • the choice of the ionic liquid may affect the degree of formation of internal olefins.
  • the ionic liquid can increase the activity of the catalyst.
  • the process of the present invention may be carried out in batch, sequential batch (i.e., a series of batch reactors) or in continuous mode in any of the equipment customarily employed for continuous process (see for example, H. S. Fogler, Elementary Chemical Reaction Engineering, Prentice-Hall, Inc., N.J., USA).
  • reaction product comprises an isomer phase comprising the internal olefin(s) and an ionic liquid phase that comprises the acid catalyst.
  • the internal olefin(s) is/are easily recoverable from the acid catalyst by, for example, decantation.
  • the separated ionic liquid phase is reused to form the reaction mixture.
  • NMR Nuclear magnetic resonance
  • GC gas chromatography
  • GC-MS gas chromatography-mass spectrometry
  • TLC thin layer chromatography
  • thermogravimetric analysis using a Universal V3.9A TA instrument analyzer (TA Instruments, Inc., Newcastle, DE) is abbreviated TGA.
  • Centigrade is abbreviated C
  • megaPascal is abbreviated MPa
  • gram is abbreviated g
  • kilogram is abbreviated kg
  • milliliter(s) is abbreviated mL(s)
  • hour is abbreviated hr
  • weight percent is abbreviated wt%
  • milliequivalents is abbreviated meq
  • melting point is abbreviated Mp
  • DSC differential scanning calorimetry
  • Potassium metabisulfite (K 2 S 2 O 5 , 99%), was obtained from Mallinckrodt Laboratory Chemicals (Phillipsburg, NJ). Potassium sulfite hydrate (KHSO 3 »xH 2 O, 95%), sodium bisulfite (NaHSO 3 ), sodium carbonate, magnesium sulfate, ethyl ether, 1 ,1 ,1 ,2,2,3,3,4,4,5,5,6,6-tridecafluoro- ⁇ -iodooctane, trioctyl phosphine, 1- dodecene, and 1-ethyl-3-methylimidazolium chloride (98%) were obtained from Aldrich (St. Louis, MO).
  • TFE pressure decreased due to the reaction, more TFE was added in small aliquots (20-30 g each) to maintain operating pressure roughly between 1.14 and 1.48 MPa.
  • 500 g (5.0 mol) of TFE had been fed after the initial 66 g precharge, the vessel was vented and cooled to 25°C.
  • the pH of the clear light yellow reaction solution was 10-11. This solution was buffered to pH 7 through the addition of potassium metabisulfite (16 g).
  • the water was removed in vacuo on a rotary evaporator to produce a wet solid.
  • the solid was then placed in a freeze dryer (Virtis Freezemobile 35xl; Gardiner, NY) for 72 hr to reduce the water content to approximately 1.5 wt% (1387 g crude material).
  • the theoretical mass of total solids was 1351 g.
  • the mass balance was very close to ideal and the isolated solid had slightly higher mass due to moisture.
  • This added freeze drying step had the advantage of producing a free-flowing white powder whereas treatment in a vacuum oven resulted in a soapy solid cake that was very difficult to remove and had to be chipped and broken out of the flask.
  • the crude TFES-K can be further purified and isolated by extraction with reagent grade acetone, filtration, and drying.
  • a 1 -gallon Hastelloy® C276 reaction vessel was charged with a solution of potassium sulfite hydrate (88 g, 0.56 nnol), potassium metabisulfite (340 g, 1.53 mol) and deionized water (2000 ml_).
  • the vessel was cooled to 7°C, evacuated to 0.05 MPa, and purged with nitrogen. The evacuate/purge cycle was repeated two more times.
  • To the vessel was then added perfluoro(ethyl vinyl ether) (PEVE, 600 g, 2.78 mol), and it was heated to 125 0 C at which time the inside pressure was 2.31 MPa.
  • the reaction temperature was maintained at 125°C for 10 hr. The pressure dropped to 0.26 MPa at which point the vessel was vented and cooled to
  • the 19 F NMR spectrum of the white solid showed pure desired product, while the spectrum of the aqueous layer showed a small but detectable amount of a fluorinated impurity.
  • the desired product is less soluble in water so it precipitated in pure form.
  • the product slurry was suction filtered through a fritted glass funnel, and the wet cake was dried in a vacuum oven (60 0 C, 0.01 MPa) for 48 hr.
  • the product was obtained as off-white crystals (904 g, 97% yield).
  • TTES-K (trifluoromethoxy)ethanesulfonate
  • a 1 -gallon Hastelloy® C276 reaction vessel was charged with a solution of potassium sulfite hydrate (114 g, 0.72 mol), potassium metabisulfite (440 g, 1.98 mol) and deionized water (2000 ml_). The pH of this solution was 5.8. The vessel was cooled to -35 0 C, evacuated to 0.08
  • a 1 -gallon Hastelloy® C reaction vessel was charged with a solution of anhydrous sodium sulfite (25 g, 0.20 mol), sodium bisulfite 73 g, (0.70 mol) and of deionized water (400 ml_). The pH of this solution was 5.7.
  • the vessel was cooled to 4 0 C, evacuated to 0.08 MPa, and then charged with hexafluoropropene (HFP, 120 g, 0.8 mol, 0.43 MPa).
  • the vessel was heated with agitation to 120 0 C and kept there for 3 hr. The pressure rose to a maximum of 1.83 MPa and then dropped down to 0.27 MPa within 30 minutes.
  • the vessel was cooled and the remaining HFP was vented, and the reactor was purged with nitrogen.
  • the final solution had a pH of 7.3.
  • the water was removed in vacuo on a rotary evaporator to produce a wet solid.
  • the solid was then placed in a vacuum oven (0.02 MPa, 140 0 C, 48 hr) to produce 219 g of white solid which contained approximately 1 wt% water.
  • the theoretical mass of total solids was 217 g.
  • the crude HFPS-Na can be further purified and isolated by extraction with reagent grade acetone, filtration, and drying.
  • a 100 mL round bottomed flask with a sidearm and equipped with a digital thermometer and magnetic stirr bar was placed in an ice bath under positive nitrogen pressure.
  • To the flask was added 50 g crude TFES-K (from synthesis (A) above), 30 g of concentrated sulfuric acid (95-98%) and 78 g oleum (20 wt% SO 3 ) while stirring.
  • the amount of oleum was chosen such that there would be a slight excess of SO 3 after the SO 3 reacted with and removed the water in the sulfuric acid and the crude TFES-K.
  • the mixing caused a small exotherm, which was controlled by the ice bath.
  • HFPS-Na hexafluoropropanesulfonate
  • the amount of oleum was chosen such that there would be a slight excess of SO 3 after the SO 3 reacted with and removed the water in the
  • the acetone was removed in vacuo to give a yellow oil.
  • the oil was further purified by diluting with high purity acetone (100 mL) and stirring with decolorizing carbon (5 g). The mixture was again suction filtered and the acetone removed in vacuo to give a colorless oil. This was further dried at 4 Pa and 25 0 C for 6 hr to provide 83.6 g of product.
  • TFES-K potassium 1 ,1,2,2-tetrafluoroethanesulfonate
  • reagent grade acetone 350 mL
  • the reaction mixture was filtered once through a celite/acetone pad and again through a fritted glass funnel to remove the KCl.
  • the acetone was removed in vacuo first on a rotovap and then on a high vacuum line (4
  • the reaction mixture was filtered once through a celite/acetone pad and again through a fritted glass funnel.
  • the acetone was removed in vacuo first on a rotovap and then on a high vacuum line (4 Pa, 25°C) for 2 hr.
  • the product was a viscous light yellow oil (103.8 g, 89% yield).
  • TFE Tetrafluoroethylene
  • Iodide (24 g) was then added to 60 ml_ of dry acetone, followed by 15.4 g of potassium 1 ,1 ,2,2-tetrafluoroethanesulfonate in 75 ml_ of dry acetone. The mixture was heated at 60 0 C overnight and a dense white precipitate was formed (potassium iodide). The mixture was cooled, filtered, and the solvent from the filtrate was removed using a rotary evaporator. Some further potassium iodide was removed under filtration. The product was further purified by adding 50 g of acetone, 1 g of charcoal, 1 g of celite and 1 g of silica gel. The mixture was stirred for 2 hours, filtered and the solvent removed. This yielded 15 g of a liquid, shown by NMR to be the desired product.
  • TPES-K 2-(perfluoroethoxy)ethanesulfonate
  • the precipitate was removed by suction filtration, and the acetone was removed in vacuo on a rotovap to produce the crude product as a cloudy oil.
  • the product was diluted with ethyl ether (100 mL) and then washed once with deionized water (50 mL), twice with an aqueous sodium carbonate solution (50 mL) to remove any acidic impurity, and twice more with deionized water (50 mL).
  • the ether solution was then dried over magnesium sulfate and reduced in vacuo first on a rotovap and then on a high vacuum line (4 Pa, 24 0 C) for 8 hr to yield the final product as an oil (19.O g, 69% yield).
  • TBP-TPES perfluoroethoxyethanesulfonate
  • the reaction mixture was heated at 60 0 C under reflux for approximately 16 hours.
  • the reaction mixture was then filtered using a large frit glass funnel to remove the white Kl precipitate formed, and the filtrate was placed on a rotary evaporator for 4 hours to remove the acetone.
  • the liquid was left for 24 hours at room temperature and then filtered a second time (to remove Kl) to yield the product (62 g) as shown by proton NMR.
  • Example 1 Isomerization of 1-dodecene in the presence of the ionic liquid 1-dodecyl-3-methylimidazolium 1 ,1 ,2,2-tetrafluoroethanesulfonate.
  • the ionic liquid i-dodecyl-3-methylimidazolium 1 ,1 ,2,2- tetrafluoroethanesulfonate (Ddmim-TFES; 2.0 g) was weighed into a small round-bottomed flask, and the flask was dried overnight at 15O 0 C under vacuum. The flask was removed from the oven, quickly stoppered, and allowed to cool in the antechamber of a dry box under vacuum before being transported into the dry box. HCF2CF 2 SO 3 H (0.5 g) and 1- dodecene (30 mL) were added to the round bottomed flask in the dry box. The flask was then lowered into an oil bath and heated for 2 hours at 100 ° C with stirring.
  • Ddmim-TFES ionic liquid i-dodecyl-3-methylimidazolium 1 ,1 ,2,2- tetrafluoroethanesulfonate
  • the ionic liquid and acid formed a separate phase at the bottom, with the product in the top phase, as shown in Figure 1 (after the material was decanted to a vial).
  • the product is colorless, i.e. water-white.
  • the GC trace of the product phase after 2 hours is shown in Figure 3; GC analysis confirmed the conversion of the 1- dodecene to the equilibrium isomers, with less than 20% of the 1- dodecene remaining.
  • Example 2 (Comparative Example): Isomerization of 1-dodecene in the absence of an ionic liquid.
  • Example 3 Isomerization of 1-dodecene in the presence of the ionic liquid 1-octadecyl-3-methylimidazolium 1 ,1 ,2,2-tetrafluoroethanesulfonate.
  • the ionic liquid 1-octadecyl-3-methylimidazolium 1 ,1 ,2,2- tetrafluoroethanesulfonate (Odmim-TFES; 2.0 g) was weighed into a small round-bottomed flask, and the flask was dried overnight at 15O 0 C under vacuum. The flask was removed from the oven, quickly stoppered, and allowed to cool in the antechamber of a dry box under vacuum before being transported into the dry box. HCF 2 CF 2 SO 3 H (0.5 g) and 1- dodecene (30 ml_) were added to the round bottomed flask in the dry box.

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  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

La présente invention concerne un procédé pour isomériser des oléfines, la réaction étant mise en oeuvre en la présence d'au moins un liquide ionique.
EP06826455A 2005-10-27 2006-10-25 Isomerisation d'olefines Withdrawn EP1954660A2 (fr)

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JP5686595B2 (ja) * 2007-05-05 2015-03-18 ビーエーエスエフ ソシエタス・ヨーロピアＢａｓｆ Ｓｅ 新規のイオン性液体
EP2261217A1 (fr) * 2009-06-10 2010-12-15 Politecnico di Milano Sels d'imidazolium de caractéristiques de cristaux liquides, utiles en tant qu'électrolytes
CN105289208A (zh) 2009-06-25 2016-02-03 Vtu控股有限责任公司 用于气体吸着的离子液体和装置的使用方法
US20130267668A1 (en) * 2012-04-09 2013-10-10 E I Du Pont De Nemours And Company Polymerization of fluorinated vinyl monomers in a biphasic reaction medium
CN102775352B (zh) * 2012-08-03 2014-10-22 山东源根石油化工有限公司 顺-12羟基十八碳烯-3-甲基-咪唑六氟磷酸盐离子液体及含有该离子液体的四冲程发动机润滑油组合物
WO2014085393A1 (fr) * 2012-11-30 2014-06-05 Elevance Renewable Sciences Procédés de fabrication d'oléfines internes fonctionnalisées et leurs utilisations
US11034669B2 (en) 2018-11-30 2021-06-15 Nuvation Bio Inc. Pyrrole and pyrazole compounds and methods of use thereof

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US2403207A (en) * 1943-03-08 1946-07-02 Du Pont Chemical process and products
JPH08509242A (ja) * 1994-02-10 1996-10-01 ビーピー ケミカルズ リミテッド イオン液体
US5958822A (en) * 1995-09-19 1999-09-28 E. I. Du Pont De Nemours And Company Modified fluorosulfonic acids
EP0787706B1 (fr) * 1996-01-30 2000-11-22 BP Amoco Corporation Procédé pour l'isomérisation des oléfines
US6395673B1 (en) * 2000-06-29 2002-05-28 E. I. Du Pont De Nemours And Company Catalyst of mixed fluorosulfonic acids
GB2383962B (en) * 2001-08-31 2005-06-01 Inst Francais Du Petrole Catalytic composition and use therefor
GB0123595D0 (en) * 2001-10-02 2001-11-21 Univ Belfast Zeolite reactions
RU2001130402A (ru) * 2001-11-13 2003-08-20 Хальдор Топсеэ А/С (DK) Способ изомеризации С5-С8 парафинового углеводородного сырья
FR2843110B1 (fr) * 2002-08-05 2004-09-24 Inst Francais Du Petrole Procede d'isomerisation d'olefines

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CN101296888A (zh) 2008-10-29
WO2007050491A3 (fr) 2007-06-14

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